WO2021234207A1 - Procédé de capture de dioxyde de carbone d'un gaz - Google Patents

Procédé de capture de dioxyde de carbone d'un gaz Download PDF

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Publication number
WO2021234207A1
WO2021234207A1 PCT/ES2021/070366 ES2021070366W WO2021234207A1 WO 2021234207 A1 WO2021234207 A1 WO 2021234207A1 ES 2021070366 W ES2021070366 W ES 2021070366W WO 2021234207 A1 WO2021234207 A1 WO 2021234207A1
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Prior art keywords
reactor
stage
liquid
gas
carried out
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Application number
PCT/ES2021/070366
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English (en)
Spanish (es)
Inventor
Alexandre Colzi Lopes
Jose Manuel ESTRADA PEREZ
Original Assignee
Trovant Technology, S.L
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Publication date
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Priority to EP21736622.8A priority Critical patent/EP4154968A1/fr
Publication of WO2021234207A1 publication Critical patent/WO2021234207A1/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1475—Removing carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1418—Recovery of products
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1425—Regeneration of liquid absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/73—After-treatment of removed components
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/84—Biological processes
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
    • C12M47/18—Gas cleaning, e.g. scrubbers; Separation of different gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/95—Specific microorganisms
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/24—Hydrocarbons
    • B01D2256/245—Methane
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/05—Biogas
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/59—Biological synthesis; Biological purification

Definitions

  • the present invention relates to a process for capturing carbon dioxide. More particularly, the present invention is encompassed in the field of processes for the improvement of a gas, and more specifically, in the processes for the capture of C0 2 by means of nitrogen microorganisms.
  • the present invention aims at capturing carbon dioxide from a gas, which may preferably contain methane, such as biogas or gases derived from petroleum, which, through the use of chemoautotrophic nitrifying microorganisms, grow and generate biomass in the process, where said biomass in turn can be reused in an anaerobic digestion process to generate the starting biogas.
  • the present invention aims to solve some of the problems mentioned in the state of the art. More specifically, the present invention describes the process for capturing carbon dioxide in a gas, intended to be carried out in at least two reactors, where said process comprises, at least, the steps of: a.) Introducing an alkaline solution in the first reactor and bubble or purify the gas so that the carbon dioxide is absorbed in the form of carbonates in said alkaline solution, forming a first liquid comprising solubilized carbonates, and as a consequence a clean gas stream is formed in an upper portion of the first reactor, b.) feeding the first liquid to the second reactor comprising in turn chemoautotrophic nitrifying microorganisms, c.) introducing a stream of air into the second reactor and a stream of nitrogen-reduced nutrients, so that Chemoautotrophic nitrifying microorganisms use the solubilized carbonates of the first liquid for their growth, thus generating solid biomass within a l resulting liquid in the second reactor.
  • a gas / alkaline solution ratio of between 0.3 to 4 can be used in the first reactor.
  • pH values in the first reactor between 6 to 12 can be used.
  • a ratio between the first liquid and the reduced nitrogen nutrients - such as ammonia - of between 5.1 to 11.5 can be used.
  • residence times of the first liquid in the second reactor can be used from a plurality of minutes to 7 days, resulting in an ammonium removal of between 25% to 100%.
  • the residence time of the first liquid in the second reactor can be from 30 minutes to 1 hour.
  • the residence time of the first liquid in the second reactor can be from 30 minutes to 3 hours.
  • Chemoautotrophic nitrifying microorganisms can be added to the second reactor initially - after or before the entry of the first liquid - so that said microorganisms do not have to be added continuously.
  • the reactor is initially inoculated with said nitrifying microorganisms and then the culture of chemoautotrophic microorganisms can grow and is maintained in the second reactor.
  • the starting gas comprising carbon dioxide can be that from combustion gases, gases derived from oil exploitation or, alternatively, a biogas.
  • the gas can be a biogas of the type produced in an anaerobic digestion process, so that consequently a portion of the biomass generated in the second reactor can be reused in the anaerobic digestion process to increase the generation of the starting biogas. object of the capture of C0.
  • residual nutrients resulting from anaerobic digestion acting as nitrogen depleted nutrients can be used in the second reactor.
  • the resulting clean gas in the upper portion of the second reactor is methane, more specifically when it is a starting gas such as biogas, natural gas or gases derived from oil exploitation that comprise methane.
  • the resulting liquid after the biomass generation is recirculated to the first reactor acting as an alkaline solution, thus improving the overall resource efficiency of the process.
  • the biomass generated in the second reactor can be recirculated out of the second reactor and returned, in order to regulate
  • the process can have an intermediate stage where the resulting liquid that is recirculated to the first reactor is previously adjusted in pH by means of a pH adjustment device.
  • Said device can be located within the first reactor or in an intermediate location between the first reactor and the second reactor.
  • the process may have an additional stage where one or more nutrients are introduced into the second reactor, to facilitate the growth of biomass from the carbonates solubilized in the first liquid.
  • Said nutrients can be selected from a list of at least one, among: ammonium, phosphorus, fertilizers, slurry, ammonium salts or urea.
  • the one or more nutrients comprise at least ammonium.
  • the liquid column of the second reactor may not be pressurized.
  • the process for capturing carbon dioxide from a gas is intended to be carried out in three reactors, where in stage a.) The gas is purified and where said process also comprises the stage of: d.) Feeding the first liquid comprising solubilized carbonates to a third reactor where the carbon dioxide absorbed in stage a.) is partially or totally desorbed, regenerating its absorbent capacity, where stage d.) takes place between stages a.) and b .) and before step c.).
  • stage d. Preferably, prior to stage d.), The following is carried out: e.) A stage of flashing the first liquid where its pressure is reduced, and optionally: f.) a stage of recirculation of a stream rich in CH 4 at the entrance of the first reactor, mixing it with the gas. Optionally after step e.), Step d.) Is carried out.
  • the desorption step d. Takes place at a temperature between 90 and 130 and C.
  • stage d. And before stage b.) The process comprises: f.) A cooling stage where the recovery of the water evaporated in stage d.) Is carried out.
  • stage c. The process comprises: g.) A stage of compensation of a stream purged in stage c.), And h.) A stage of feeding said stream compensated in stage g.) Before of stage a.).
  • Figure 1. Shows a schematic view of a preferred embodiment of the process for capturing carbon dioxide in a gas.
  • Figure 2. Shows a schematic view of a preferred embodiment of the process for capturing carbon dioxide from biogas from anaerobic digestion.
  • Figure 3. Shows a schematic view of a preferred embodiment of the process when there is an intermediate desorption stage.
  • Figure 1 shows a schematic view of a preferred embodiment of the process for capturing carbon dioxide in a gas. More in particular, figure 1 shows that said is intended to be carried out in two reactors (1, 2), and presents a first stage that comprises bubbling the gas in the first reactor (1) which in turn comprises a solution alkaline (4), so that the carbon dioxide is absorbed in the form of carbonates in said alkaline solution (4) forming a first liquid (6), and as a consequence a stream of clean gas (5) is formed in an upper portion of the first reactor (1).
  • Said clean gas (5) can be methane in a preferred embodiment where the starting gas (3) is a biogas, or gases derived from oil, not being the case in, for example, combustion gases.
  • the process comprises a successive stage to feed the first liquid (6) to the second reactor (2) which in turn comprises chemoautotrophic nitrifying microorganisms (7), where said second reactor (2) It further comprises an air inlet (9) and a source of a nitrogen-reduced nutrient source (8) which in the described preferred embodiment comprise at least ammonium.
  • the chemoautotrophic microorganisms (7) use the carbonates of the first liquid (6) for growth, thus generating solid biomass (12) within a resulting liquid (11) contained in the second reactor (2).
  • the process also comprises recirculating the resulting liquid (11) to the first reactor (1) acting, as well as the alkaline solution (4) necessary to solubilize the carbon dioxide in the form of carbonates .
  • the biomass (12) can be recirculated out of the reactor and subsequently returned in order to keep the nitrifying biomass constant.
  • the resulting liquid (11) is adjusted in pH by means of the device (14) before being introduced into the first reactor (1) and located between the first reactor (1) and the second reactor (2).
  • the biomass (12) is recirculated out of the second reactor (2) through the device (14) before returning to said second reactor (2).
  • Figure 2 shows a schematic view of a preferred embodiment of the process for capturing carbon dioxide in a biogas (3 ') from anaerobic digestion (15).
  • figure 2 shows that the process in a second preferred embodiment comprises reusing a portion (12 ') of the biomass (12) generated in the second reactor (2) in the anaerobic digestion (15) to in turn produce the starting biogas, improving the overall efficiency of both processes in synergy.
  • the biomass (12) generated in the second reactor (2) allows to increase the production of biogas and avoids the need to manage waste and sludge of said excess biomass (2).
  • the process further comprises using residual nutrients (8) resulting from anaerobic digestion (15) and introducing said residual nutrients (8) into the second reactor, thus acting as the source of nutrients (8) reduced nitrogen and taking advantage of even more the global efficiency in the resources used in both processes.
  • the resulting liquid (11) is adjusted in pH by means of the device (14) which in turn is located inside the first reactor (1).
  • the biogas (CH 4 + C0) enters the system, is compressed in a first compressor (23) and enters the lower part of the first reactor (1) or scrubber type absorption column.
  • the gas rises and comes into contact with an alkaline liquid solution containing carbonates (sodium or potassium carbonate solution).
  • the C0 2 of the gas is transferred to the liquid solution, obtaining in the head of the first reactor (1) a stream of purified CH 4 (biomethane).
  • the key operating parameters of this unit are operating pressure (range 2 to 15 bar), gas and liquid velocity, and gas / liquid ratio.
  • the liquid rich in C0 2 collected at the bottom of the first reactor (1) is directed to an optional flashing unit (14) in which the pressure is reduced in order to subsequently desorb the methane CH 4 that may have been absorbed in the liquid.
  • This gas stream rich in CH 4 can be recirculated from the head of the flashing unit (14) to the inlet of the system and mixed with the fresh biogas, minimizing the losses of CH 4 .
  • the liquid stream rich in C0 2 obtained at the bottom of the flashing unit (14) is directed to the head of a third reactor (13) or desorption column.
  • the liquid trickles from the top and at the bottom, temperature is applied by means of a heat exchanger (15) or electrical resistance to increase the temperature of the liquid.
  • the C0 2 absorbed in the alkaline liquid carbonate solution in the first reactor (1) is partially or totally desorbed, regenerating its absorbent capacity.
  • the key operating parameter of the desorption column is the operating temperature in the column (90 - 130 e C).
  • a gaseous stream of C0 2 is obtained , which passes through a cooling system (16) or condenser to recover the water that may have evaporated in the desorption.
  • This stream is mixed with air (17) and fed by bubbling, after passing through a second compressor (18), to the second reactor (2) or nitrification tank in which nitrifying microorganisms can use C0 2 as a carbon source. .
  • the C0 2 stream and the air stream could not be mixed, feeding separately to the second reactor (2) or nitrification tank.
  • This second reactor (2) is also fed with nutrients (19) and ammonia necessary for biological activity.
  • Part of the liquid stream (22) of alkaline carbonate solution obtained at the bottom of the first reactor (1) or absorption column can be purged towards the second reactor (2) or nitrification tank (as it loses absorbent capacity), and it serves as a source of C0 2 dissolved in the liquid to feed the nitrifying microorganisms.
  • the purged stream is compensated in the system by feeding fresh carbonate solution from a tank (20) in which a new reagent solution is prepared using water, already free of C0 2 (21) from the second reactor ( 2) or nitrification tank. This regenerated liquid stream is fed back to the head of the first reactor (1) or absorption column, closing the cycle of the liquid phase.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Analytical Chemistry (AREA)
  • Biomedical Technology (AREA)
  • Environmental & Geological Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Zoology (AREA)
  • Biotechnology (AREA)
  • Bioinformatics & Cheminformatics (AREA)
  • Organic Chemistry (AREA)
  • Wood Science & Technology (AREA)
  • Microbiology (AREA)
  • Biochemistry (AREA)
  • General Engineering & Computer Science (AREA)
  • General Health & Medical Sciences (AREA)
  • Genetics & Genomics (AREA)
  • Sustainable Development (AREA)
  • Molecular Biology (AREA)
  • Gas Separation By Absorption (AREA)
  • Treating Waste Gases (AREA)
  • Apparatus Associated With Microorganisms And Enzymes (AREA)

Abstract

L'invention concerne un procédé de capture de dioxyde de carbone d'un gaz (3), destiné à être mis en œuvre dans deux réacteurs (1,2), et qui consiste à introduire une solution alcaline (4) dans le premier réacteur (1) et à produire des bulles avec le gaz (3) de façon que le dioxyde de carbone soit absorbé sous forme de carbonates dans ladite solution alcaline (4) formant un premier liquide (6), un courant de gaz méthane (5) étant formé par conséquence dans une partie supérieure du premier réacteur (1) ; alimenter le premier liquide (6) dans le deuxième réacteur (2) qui comprend des micro-organismes nitrifiants chimioautotrophes (7) ; et introduire un courant d'air (9) dans le réacteur (2), de façon que les micro-organismes autotrophes (7) utilisent les carbonates du premier liquide (6) pour leur développement, générant ainsi une biomasse solide (12) à l'intérieur d'un liquide résultant (11) dans le deuxième réacteur (2).
PCT/ES2021/070366 2020-05-22 2021-05-21 Procédé de capture de dioxyde de carbone d'un gaz WO2021234207A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP21736622.8A EP4154968A1 (fr) 2020-05-22 2021-05-21 Procédé de capture de dioxyde de carbone d'un gaz

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
PCT/ES2020/070339 WO2021234191A1 (fr) 2020-05-22 2020-05-22 Procédé pour la capture du dioxyde de carbone présent dans un gaz
ESPCT/ES2020/070339 2020-05-22

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WO2021234207A1 true WO2021234207A1 (fr) 2021-11-25

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PCT/ES2021/070366 WO2021234207A1 (fr) 2020-05-22 2021-05-21 Procédé de capture de dioxyde de carbone d'un gaz

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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4372856A (en) * 1981-03-30 1983-02-08 Morrison Jon R Process and system for anaerobic treatment of waste
WO2011014507A1 (fr) * 2009-07-27 2011-02-03 The University Of Wyoming Research Corporation Systèmes et procédés de traitement de combustible propre biologique
WO2011139804A2 (fr) * 2010-04-27 2011-11-10 Sequesco Utilisation de microorganismes d'oxyhydrogénation pour la capture de carbone non photosynthétique et la conversion de sources de carbone inorganique et/ou ci en composés organiques utiles
EP2556881A1 (fr) * 2011-08-11 2013-02-13 Nederlandse Organisatie voor toegepast -natuurwetenschappelijk onderzoek TNO Combinaison de culture d'algues et capture de CO2
WO2013034947A1 (fr) * 2011-09-08 2013-03-14 Cellennium (Thailand) Company Limited Valorisation de biogaz en méthane purifié commercialisable exploitant la culture de microalgues
US20160030884A1 (en) * 2013-03-14 2016-02-04 The University Of Wyoming Research Corporation Conversion of Carbon Dioxide Utilizing Chemoautotrophic Microorganisms Systems and Methods

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4372856A (en) * 1981-03-30 1983-02-08 Morrison Jon R Process and system for anaerobic treatment of waste
WO2011014507A1 (fr) * 2009-07-27 2011-02-03 The University Of Wyoming Research Corporation Systèmes et procédés de traitement de combustible propre biologique
WO2011139804A2 (fr) * 2010-04-27 2011-11-10 Sequesco Utilisation de microorganismes d'oxyhydrogénation pour la capture de carbone non photosynthétique et la conversion de sources de carbone inorganique et/ou ci en composés organiques utiles
EP2556881A1 (fr) * 2011-08-11 2013-02-13 Nederlandse Organisatie voor toegepast -natuurwetenschappelijk onderzoek TNO Combinaison de culture d'algues et capture de CO2
WO2013034947A1 (fr) * 2011-09-08 2013-03-14 Cellennium (Thailand) Company Limited Valorisation de biogaz en méthane purifié commercialisable exploitant la culture de microalgues
US20160030884A1 (en) * 2013-03-14 2016-02-04 The University Of Wyoming Research Corporation Conversion of Carbon Dioxide Utilizing Chemoautotrophic Microorganisms Systems and Methods

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WO2021234191A1 (fr) 2021-11-25
EP4154968A1 (fr) 2023-03-29

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